Hydrocarbon conversion process



Patented Aug. 14,1945

No Drawing. Application November 27, 1944,

Serial N0. 565,422 a i Claims. (ei. 2c0 ss3.4)

This invention relates to a process for the alkylation of saturated organic compounds with olefines and to improved catalysts for accelerating said reaction. Additionally, this; invention relates to a process for the isomerization of saturated or ganic compounds and the alkylation of the resulting isomerized organic compounds with olefines and to improved catalysts for accelerating said reactions. In one specific embodiment thereof, this invention relates to a process for thealkylation of isoparamns with olefines and to improved catalysts for accelerating said: reaction. In another specific embodiment thereof, this invention relates to the isomerization of normal paraflins toisoparaffins and the alkylation of the resulting isoparaflins with olefines and to improved catalysts for accelerating said reactions.-

This applicationis in part a continuation of my copending application, Serial Number 427,171, filed January 17, 1942, which in. turn is inpart a continuation of application, Serial Number 296,807, filed September 27, 1939, now UVS Patent 2,271,956, issued February 3, 1942.

It is an object of this invention to provide an improved process for the alkylation. of saturated organic compounds with olefines and to-provide improved catalysts for accelerating said reaction. Additionally, it is an object of this invention to provide an improved process for theisomerizatic-n of saturated organic compounds and. the alkylation of the resulting i'somerized organiccompounds with olefines and to provide improved catalysts for accelerating saidreactionsl,

It is a further object of this inventionto provide an improved process for the alkylation-of isoparaillns with olefines and toprovide improved catalysts for accelerating said reaction. a

It is anotherobject of thisinventionto provide an improved process for the isomerization. of nor.-v mal paraffins to isoparafiins andthe alltylation of the resulting isoparaflins with olefines. andto improved catalysts for accelerating. said reactions.

It is well knownin the arttc. alkylat v saturated organic compounds with olefines. For example,

it is well known in the art to alkyiate isoparaffins with olefines. As a'speciflc example of .such a. re,- action, the alkylation of.'isobutane with olefines containing four carbon atoms to the molecule may be cited. Numerous catalystshave been proposed for this reaction. Among.. these maybe mentioned concentrated sulfuric acid, bothv alone and sulfuric acid promoted with boron fluoride or metal salts, such as salts ofm' ercury, nickel, silver. copper n lt -conce t at pa e phoric acid promoted as above or not as desired";

mixtures of concentrated sulfuric acid and concentrated phosphoric acid promoted as above or not as desired; aluminum halides, especially aluminum chloride and aluminum bromide, promoted if desired bya trace of water, hydro en halide, alkyl halideor the like; anhydrous hydrogen fluoride; boron fluoride, promoted if desired with a trace of water, hydrogen fluoride, nickel or H mixtures of said promoters and similar catalysts.

brings about secondary reactions.

All catalysts proposed to date have various disadvantages. .The. mineralwacids, for example, bring about secondary reactions to a considerable: extent. This not only destroys an appreciable amount of the charge but more serious, contain-- catalyst. Aluminum bromide is very expensive and also bringsabout secondary reactions; ,Boron fluoride is veryexpensive, 3

Also, it is well know'njin thelartto is'omerizc saturated or'ganic compounds. For example, it is well known in thearttoisomeriZe normal paraflins containing fouror more carbon atoms to isoparafiins. As a specific, example of such a frea action, the isomerizatior'rofv normal butane to. isoj-Y i butane maybev cited. Several catalysts have been proposed for acceleratingthis reaction, j most of these being an'a-lumiruimhalide,v especially aluminum chloride or aluminum bromide, either alone. or supported on or united with another. K1351 terial- Such catalystsare usually promoted with; a trace of water, hydrogen halide-or the like. These catalysts have various disadvantages. hid! minum chlorideis not soluble to any extent in the reactant and .hence is not very active; 'Since only the surface ofthecataly tpa t c esj a fect ve; the catalyst is'not'eflicie'ntly used. Additionally, this halide brings about secondary reactions wasteful of reactants and destructive of catalyst. Aluminurn bromide is" very' expensive and also lhave found that alkyl aluminumhal'ides are cheap and effective catalysts for promoting the alkylation and 'isomeri zation reaction's aboveide scribed and'others ,of a similar nature. Alkyl aluminum hali'des are'efiective in promotingthe alkylation of saturated organic compounds with olefines." 'Alkyl aluminum halides are effective'in' promoting the isomerization of normal paraflins containing four or more carbon atoms to isoparaffins. Alkyl aluminum halides are soluble in most organic liquids.

Additionally, when using prior art catalysts, the alkylation of isobutane with propylene and more especially with ethylene has been found to proceed extremely slowly. When employing alkyl aluminum halides however, these lower olefines react rapidly. This is highly advantageous since in prior art processes, which are essentially limited to the alkylation of isobutane with olefines containing four carbon atoms, isooctanes are formed. While these are valuable components in aviation blends, the volatility is-low. For use in aviation gasoline, isooctanes must be blended with other materials of higher volatility. Highly volatile materials possessing at the same time the requisite high octane number are available only in limited amounts. However, by thealkylation of isobutane with, for example, ethylene, using the catalysts of the instant invention, branched chain hexanes are formed. These have a high octane number and high volatility and are excellently suited for blending with isooctane. The same'applies to the branched chain heptanes resulting from the alkylation of isobutane with propylene, using the catalysts of the instant invention.

Alkyl aluminum halides are conveniently prepared. The most general method of preparation involves the interaction of metallic aluminum and an alkyl halide as described by Grignard and Jenkins (Bull, IV, 37, 1376, 1925) and Leone (Gazz. chim. ital., 55, 294, 1925) Detailed directions for the laboratory preparation of alkyl aluminum halides by this method were subsequently given by Hnizda and Kraus (J. Amer. Chem. Soc., 60, 2276, 1938). It is seen that this method is very general, being capable theoretically of producing all alkyl aluminium halides. However, it is very expensive, requiring the use of alkyl halides.

A somewhat less general but very economical method for the preparation of alkyl aluminum containing appreciable hydrogen, over metallic aluminum or activated metallic aluminum.

For the better'understanding of this invention reference may be had to the following illustrative but non-limiting examples thereof.

Example 1 A mixture consisting essentially of normal butane and isobutane was brought to a temperature} of 550, C, and passedjpver a -catalyst consisting of 10% chromium oxideon activated alumina. About of the charge was converted to olefines. The reaction products obtained by the catalytic dehydrogenation of the isobutane-normal butane mixture were subjected to a conventio'nal absorption-stripping operation. Hydrocarbons of four carbon atoms were essentially completely absorbed in a hydrocarbon absorption oil and the resulting rich oil was stripped of these by fractionation under pressure. The resulting gas contained 60% isobutane, 21% normal butane,

14% 'isobutene' and 5% normal butenes on a 100% pressed to a pressure of1 000 pounds per square halides has been described by Hall and Nash (J. Inst. Pet. Tech., 23, 679, 1937) involving contacting an olefine with a mixture of aluminum halide and metallic aluminum. I have found, as set forth in my patent previously mentioned, that this reaction proceeds much more rapidly and smoothly and higher yields of alkyl aluminum halides are obtained if the olefine is mixed with appreciable hydrogen prior to contacting with the aluminum halide-aluminum metal mixture or if activated metallic aluminum is employed. Especially good results are obtained if the olefine is mixed with hydrogenin appreciable amounts and activated metallic aluminum is employed. Obviously, it is impossible to prepare methyl aluminum halides by this general method but if aluminum chloride is used as the aluminum halide the process serves as a very economical source of alkyl aluminum chlorides higher than the methyl derivatives.

Alkyl aluminum halides may also be made by a variation of the above process involving passage of a hydrogen halide over metallic aluminum or preferably activated metallic aluminum following which an olefine, preferably in admixture with appreciable hydrogen, is passed over the resulting mixture to form the desired alkyl aluminum halides. or, alkyl aluminum halides may be prepared by passinga mixture of a hydrogen halide and an olefine, said mixture preferably inch, heated to 150 C. and'passed over'an intimate mixtu-reo'f" aluminum chloride and pow-' dered activated metallic aluminum'in equimolecular proportions. The resulting liquid product was divided into two"porti0ns. One portion was added to normal butane tocatalyze the isomeriza tion thereof and the mixture was held at 25 C. to 50 C. for a period of 'one week with occasional shaking. of the original normal butane had been isomerized to isobutane and the resulting mixture was employed as chargein the previously described catalytic dehydrogenation step. The second portion was added to the reaction products of four car-T bon atoms obtained from the catalytic dehydrogenation step by absorption-stripping to catalyze the alkylationpf isobutane with isobutene and normal butenes. A yield of 183% isooctanes based on olefines was obtained.

As is evident, the small amount of gaseous 01efinic byproducts obtained in the catalytic dehy drogenation of the reaction mixture obtained by the isomerization of normal butane is employedto product the catalyst required to isomerize the normal butane chargeand to alkylate the isobutanef ormedfby said i'somerization with the butenes produced; by catalytic dehydrogenation.

For each volumes'of normal butane isomerized" and dehydrogenated there. were obtained about 15 volumes of hydrocarbons of less than fourcarbon atoms to the molecule and IOO volumes of hydro gen. The hydrocarbons of lessthan four carbon atoms to the molecule were about 50% olefines, mostly ethylene' Onf converting these lower olefines to alkyl aluminum halides there was formed suflicient catalyst to sustain both the isomerizae tion and alkylation 'reactions. these lower olefines to catalyst there is much more hydrogen presentthanis required for best results (actually, hydrogen is not essential) so most or all of the hydrogen maybe discarded before making the catalyst] Preferably, however, for each volume of olefineat least.0.5 volume of hydrogen is retained. If it is inconvenient to dis-. cardpart or all of the hydrogen it is not necessary'todoso l In the above 'e'xa ple, is'omerization was con} ducted under very mild conditions and a longtime for reaction was required. If-desired, higher oper- At the end of this period some 75%.

In converting uct-was also' comparatively mild.

, 120 0. or even up to 150 C. Obviously, above 15310. (the critical temperature of isobutane): vapor phase conditions prevail and this occurs even at'lower' temperatures such as'have been mentioned unless superatmospherlc pressure is employed. i i i 1 'I'he dehydrogenation of the isomerized'prod- For each 100 volumes of gas charged there were obtainedabout 60 volumes of isobutane, 2l.volumes normal butane, 20'volume's' hydrogen,"14 volumes isobutene, volumes normal butenesand 3 volumes of hydrocarbons of less than-tour carbon atoms to themolecule. .Such a gas mixture, especially after removal of hydrogen and, if desired, hydrocare bons 'of less than 4 carbon atoms to the molecule, is an excellent 'alkylation charge since the isobuta'ne/olefine ratiois high which is every desirable in alkylation since oleilne polymerization is thereby retarded. However, if desired, a portion, for example, one half, of'the isomerized product may be dehydrogenated under more severe 'conditions than those described, for example; at a higher temperature and/or longer contact time and the products may, aiter hydrogen removal and; if desired, removal of hydrocarbons of less than four carbon atoms to the molecule, be mixed with'th'e untreated isomerized mixture-and the whole'subjectedto alkylation. 'When operating in this manner the. dehydrogenation selectivity is somewhat impaired, i. e. the yield of hydrocarbons ofless than four carbon higherthan before. I

atomsis somewhat Obviously, after alkylation, theyunreacted'hy- I A predominantly parafllnic heavy naphtha haymga boiling range 01' 246-415 F. was mixed with 5 mole percent of'ethyl aluminum dichloride and diethyl aluminum chloride in approximately equimoleculars proportions. The whole was heated to 400 F. and material boiling lower than the heavy naphtha charge was removed from the reaction mixture as formed and was separated into a gase'ous component, largely isobu-tane, and a liquid component, isoparamnic light naphtha. The gaseous component was catalytically dehydrogenated as described in Example 1 except that a catalyst consisting of 6% molybdenum oxideon activated alumina was employed. The dehydrogenated gaseous products were worked up as described in Example 1. The hydrogen and gaseous hydro carbons containing less than iour carbon atoms to the molecule obtained as byproducts from the catalytic dehydrogenation of the gaseous com-Y ponent were compressed to 1000 pounds per square inch,'hea,t'ed to 150 C. and passed over an lnti-' mate mixture of aluminum chloride and activated metallic aluminum in equimolecular proportions.

The resulting liquid product, the essential ingreclients of which comprised primarily ethyl alumi-' num dichloride and diethyl aluminum chloride, was divided into two portions. The resulting porexample, 'isobutanef obtained from the heavy;

tions .were distributed-as indicated in Example 1, one: was iaddedtothe; fresh heavy naphtha. charge-to catalyze the' destructive isomerization' thereof. and ..the other was added to the reaction: products ot-four carbon atoms from the catalytic. dehydrogenation step tocatalyze thealkyla'tionnt' isobutane with normal butenes and isobuteneiaspreviously described in' Example -l. i -The blend of i the. resulting isooctane-and the =isoparafllnic: light naphtha. fromzdestructive. isomerization of heavynaphthacharge forms an excellent aviation fuelri 4 i i i Emmple SimilartoExample 2.. It. hasbeen found that in the destructiveisomerization of heavy naphtha, at elevated temperatures in the presence "of alkyl aluminum halides the-ratio of isobutane to,iso-, parafilnic ligh-tnaphtha formed can be-widely varied at will by conducting the reaction 'in the, presence of more or lessahydrogen, especially hy drogen under pressure. As the amount of hydro-y gen i increased, isobu-tane production declines.- Hydrogen from any convenient source may: be' employed, ior'examp1c, hydrogen obtained as by-w productin the catalytic dehydrogenation o1" the gaseous component aspreviously described. It the hydrogen thus produced plus lower gaseous: hydrocarbons is passed Over; aluminum halide-n metallic 1 aluminum (or activated metallic aluminum) mixture to produce alkyl aluminum halides as described in Examples -1 and2 then the hydro-1 mentionedthe amount and pressure of hydrogen determines in large; measure the isobutane-light isoparafllnic naphtha ratio in the products. -If

the treatment of heavy naphtha is carried out in.

the presence of 5 to lo moles of hydrogen per mole of heavy naphtha at moderately elevated to high superatmospheric pressure," say 750 pounds per square inchor more; isobutane production-is practicallynil. Onthe other hand, if no hydro-v genis used, about two moles of isobutane are producedper ,molegof isoparai'finic light naph'tha at thetemperature specific, the molecular weight of the isoparaifinic light naphtha being calculated as will be described below. Obviously, if a large. amount ofhydrogen is recycled it mustbe ob tained from a sourceother than the products fromthe r ziatalyidc dehydrogenatic of isobutane, since little or no isobutane forms. Usually however, hy-

drogen is employed to regulate, notprevent isobutane production' v. i a

I Example 4 1 ,Similart'o Exam l s. .It'has been found that} in destructive isomerization of heavynaphtha. atelevated teniperatures. mine .presence ofalkyl aluminum halides the ratio of isobutane to iso- Q parafiinic lightfnaphthaformed can be widely. v'aried at willby conducting the. reaction in the presence of. more or less isobutane, especiallylsobutane under pressure. As the amoun-tof isobu tane added to the charge is increased, isobutane production from the charge decreased Isobutan e from anyv convenient source may be employed, fornaphtha .by destructive isomerizationQ As. men:

tioned... the f amount and pressure of Q isobutane adde'dito the heavy naphtha charge. determinesin large measure the amount, of-isobutan emade. bythe charge. Ii the treatment of-heavy'naphtha-g i carried; out in the 7 presence of l. to -afmole's. of. isobutane per (mole of heavy naphtha. at. modem]. ately elevated to 'high superaimos nenc pressure,

say 750 I pounds 'per square inchor more; .isobutane production ispra'cticailly 'nil." If on the other hand, no isob'utane is added-about .two'moles of isobutane are produced-permole of is'oparafiini'c' light naphtha produced at the temperature spec ified, the molecular weight of the isoparafiinid light naphtha being calculated-as will be described below. Obviously, if a large amount of isobutane is recycled it must be obtained from a source other than the destructiveisomerization of the hea'vynaphtha charge since" under suchcconditions no isobutane forms. Usually, however, isobutane is recycled to-regulate,- not prevent, isobutane production.

" Obviously, in' -Examples -3 ,and' l; isobutane production maybe regulated or practically prevented by recycling a mixture of hydrogen and isobuta'ne instead ofl'either gas separat'ely.-

iI-Iavy naphtha and light naphtha, being mixtures, have no true molecular weight but the approximateaverage molecular weights maybe determined '01 may be calculated from empirical charts familiar to petroleum technologists; It

is thisaverage molecular weight thatiis usedjin the three previous examples. v H

Thede'structive isomeriz'atiorr of'heavy naph th'a described in the previous three'exa'mples may be conducted in the approximate temperature range" 200 {500'F'. more or less."

While "in the above examples the alk'ylation of isobutane with gaseous olefines has been 'de-' scribed, the invention i not limited thereto. Any isoparaflin containing a tertiary hydrogen atom,-

that is ahydi'ogen atomat'tached to a carbon atom which in turn is' 'attachd' to three other carbonatoms','may be employed;

Also; liquid olefin'es "ma'y be femployedas the allsylating componentf Among j these 'ma'y be mentioned, catalytic 1 polymer gasoline, cracked gasolines', reformed naphthas and cracked wax distillates. 'Also, gaseous olefines from any con: venient source may be employed as the alkylati'on component of therea'ction mixtura'for' example,

the gaseous 'olefines in refinery gases obtained from "cracking, reforming and other operations. 'As' has" been indicated previously, the catalyst;

for 'the "isomerization and al kylatio n reactions maybe-prepared without the'use of an aluminum halide by the interaction or an 'olefine, a hydrogenfhalide andfmetallic aluminum or activated? metallic aluminum; preferably in the presene'of;

hydrogen.

the exacta'mount'of heating orwcooling necessary be: accomplished at low superatmospheric pressureor atmospheric-"pressurer .2 I Obviously, .in anyizs'cheme for the preparation of alkyl aluminumihalides the metallic aluminum or activated metallic aluminum sooner or later becomes-exhausted. If it 'i's'gdesired to produce catalyst continuously' it' is necessary to provide two orfimore reactors at leastone of which 'isal-' ways on stream :while a at least another. is being repacked with the necessary. reactant or reactants and. is generally. being made ready for putting on stream when theizcontents of the reactor. or. reactors on stream become exhausted. Obviously;

in: the alternate procedure" for the production ofcatalyst involving first, the formation of the aluminum halide-metallic aluminum or activated metallic aluminum mixture followed by second, passing the ,olefine or f olefine-hydrogen mixture, two-reactors at-least'are required? for continuous production of catalyst. However,-as will:be evident-to those-skilled'in the art, con'tinuo'usproduction of catalyst is not essential 'in 'the' process of the instant invention; i

It hasbeen found that-alkyl aluminum halides do not 'require" activation *withwtrac'e's of water, hydrogen halides, alkyl halides and the like :as is commonly required withaluminum halides. It is believed however that perhaps traces of water in The necessary hydrogen halide may be obf tained from known sources or itmay be pre pared by the union of part or all of the hydrogen formed in the catalytic dehydrogenation step witha halogen, for example, chlorine. For the olefine" componentQthe hydrogen gases obtained in-thecatalytic dehydrogenation step that contain a lesser number of carbon atoms than the charge may be used. U Obviously, olefines from other sources may be employed if desired.

The mixture containing the hydrogen halide and the olefineor the twoseparately may be compressed-to say 20 to 200 atmospheres, preferably about '35 atmospheres and then passed through a reactor filled'with metallic aluminum or activated metallic aluminum which may be in the form or; powder (preferably formed into pellets), scrap,

turnings, sheet, shot, foil or any other suitable forms Hydrogenis preferably added to the gaseous reactants. The operating temperature may be maintained in the range -400 C., preferably '150-350j C The reactionfis exothermic so cooling maybe required under steady conditions,

the hydrocarboncharge may 1 react; with a small portion of thecatalyst and thus bring about'so'me" degree of.:activation-of the. whole Be it remembered that whileth instant invention has been described gby means of certain specific examples thereof it is tobe understood that these are illustrative only and .the scopevofsaid inventionis sw m s 'waylimited to the dis closures of;fsuch speciiic examples] thereof. v

Iclaimg. v,

1,, The hydrocarbon cbnqrsan' including subjecting a charge ;con prising; an isopar-- afilrito catalytic dehydrogenation, separating the resulting reaction mixture into; a f rst fraction comprising hydrocarbons o f ,the same .number o f,"carbon atoms as the; isoparaffin charge and a second fraction comprising hydrogen and hydrocarbon s oi'a lesser numberof ,carbon atoms than/the isoparallin. charge, contacting said sec- 0nd fractionwith a mixture of aluminum halide and metallic aluminum to. form alkyl aluminum ames; add catalytic}; amounts of said alkyl aluminum halides to said, first fraction to accelerate the ,a'lkyla'tion ojfQ unconverted isopare ailin charge by the olefines, therein.

25,; eprocess of claim ,1, further characterized byfthejfac tfthat said metallic aluminum is activated. 1...

3. ;che, process of. claim 1 further characterized by I the l fact that said aluminum halide is alumiareiorme r a e? asi.m mnaaesz num chloride whereby alkyl. aluminum 1 chlorides by the fact that said metallic aluminum is activated and said aluminum halide is aluminum chloride whereby alkyl aluminum chlorides are formed.

5. The hydrocarbon conversion process including subjecting a charge comprising an isoparafiln to catalytic dehydrogenation, separating the resulting mixture into a first fraction comprising hydrocarbons of the same number of carbon atoms as the isoparafiin charge and a second fraction comprising hydrogen and hydrocarbons of a lesser number of carbon atoms than the isoparafiin charge, contacting said second fraction with a. mixture of aluminum halide and metallic aluminum to form alkyl aluminum halides, adding a first catalytic portion of said alkyl aluminum halides to said first fraction to accelerate the alkylation of unconverted isoparafiln charge by the olefines therein, adding a second catalytic portion of said alkyl aluminum halides to a charge comprising a normal parafiln containing at least four carbon atoms to accelerate the isomerization thereof to an isoparafiin and charging the resulting isomerizate to the catalytic dehydrogenation step.

6. The process of claim 5, further characterized by the fact that said metallic aluminum is activated.

7. The process of claim 5, further characterized by the fact that said aluminum halide is aluminum chloride whereby alkyl aluminum chlorides are formed.

8. The process of claim 5, further characterized by the fact that said metallic aluminum is activated and said aluminum halide is aluminum chloride whereby alkyl aluminum halides are formed.

9. The hydrocarbon conversion process including subjecting a charge comprising isobutane to catalytic dehydrogenation, separating the resulting reaction mixture into a first fraction comprising hydrocarbons of four carbon atoms and a second fraction comprising hydrogen and hydrocarbons of less than four carbon atoms, contacting said second fraction with a mixture of aluminum halide and metallic aluminum to form alkyl aluminum halides and adding catalytic amounts of said alkyl aluminum halides to said first fraction to accelerate the alkylation of unconverted isobutane by the olefines therein.

10. The process of claim 9, further characterized by the fact that said metallic aluminum is activated.

11. The process of claim 9, further characterized'by the fact that said aluminum halide is aluminum chloride whereby alkyl aluminum chlorides are formed.

12. The process of claim 9, further characterized by the fact that said metallic aluminum is activated and said aluminum halide is aluminum chloride whereby alkyl aluminum chlorides are formed.

13. The hydrocarbon conversion process including subjecting a charge comprising isobutane to catalytic dehydrogenation, separating the resulting reaction mixture into a first fraction comprising hydrocarbons of four carbon atoms and a second fraction comprising hydrogenand hydrocarbons of less than four carbon atoms contacting said second fraction with a mixture of aluminum halide and metallic aluminum to form alkyl aluminum halides, adding a first catalyticportion of said alkyl aluminum halides to said first fraction to accelerate the alkylatlon of unconverted isobutane'by the olefines therein, adding a second catalytic portion of said alkyl aluminum halides :to a charge comprising normal butane to accelerate the isomerization thereof to isobutane and charging the resulting isomerizate to the. catalytic dehydrogenation zone.

14. The process of claim 13, further characterized by the fact that said metallic aluminum is activated.

15. The process of claim 13, further characterized by the fact that said aluminum halide is aluminum chloride whereby alkyl aluminum-chlorides are formed.

16. The process of claim 13, further characterized by the factthat said metallic aluminum is activated and said aluminum halide is aluminum chloride whereby alkyl aluminum chlorides are formed. I

1'7. The hydrocarbon conversion process in-, cluding subjecting a charge comprising isobutane to catalytic dehydrogenation, separating the resulting reaction mixture into a first fraction comprising hydrocarbons of four carbon atoms and a second fraction comprising hydrogen and hydrocarbons containing less than four carbon atoms, contacting said second fraction with a mixture of aluminum halide and metallic aluminum to form alkyl aluminum halides, adding a first catalytic portion of said alkyl aluminum halides to said first fraction to accelerate the alkylation of unconverted isobutane by. the olefines therein, adding a second catalytic portion of said alkyl aluminum halides to heavy naphtha to accelerate the conversion thereof to light isoparafiinic naphtha and isobutane and .charging the resulting isobutane to the catalytic dehydrogenation step.

18. The process-of claim 17, further characterized by the fact that said metallic aluminum is, 

